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WO2015007343A1 - Procédé et dispositif d'obtention d'une composition contenant des hydrocarbures à partir de résidus - Google Patents

Procédé et dispositif d'obtention d'une composition contenant des hydrocarbures à partir de résidus Download PDF

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Publication number
WO2015007343A1
WO2015007343A1 PCT/EP2013/065329 EP2013065329W WO2015007343A1 WO 2015007343 A1 WO2015007343 A1 WO 2015007343A1 EP 2013065329 W EP2013065329 W EP 2013065329W WO 2015007343 A1 WO2015007343 A1 WO 2015007343A1
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WO
WIPO (PCT)
Prior art keywords
fluid
evaporator
processing plant
hydrocarbon
reactor
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2013/065329
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German (de)
English (en)
Inventor
Wolfgang Spiess
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
CATALYTEC
Original Assignee
CATALYTEC
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by CATALYTEC filed Critical CATALYTEC
Priority to PCT/EP2013/065329 priority Critical patent/WO2015007343A1/fr
Publication of WO2015007343A1 publication Critical patent/WO2015007343A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0064—Feeding of liquid into an evaporator
    • B01D1/007—Feeding of liquid into an evaporator the liquid feed being split up in at least two streams before entering the evaporator
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/008—Liquid distribution
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/40—Thermal non-catalytic treatment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • C10G2300/1007—Used oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel oil
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the invention relates to a method and an apparatus for obtaining a hydrocarbon-containing composition from a
  • DE 10 2005 056 735 B3 discloses the process for producing diesel oil from hydrocarbon-containing residues in a mixed substance cycle with solids separation and product distillation for the diesel product.
  • the substance mixture is an oil, residue and
  • Hydrocarbons which are split by means of the catalyst in suitable short-chain hydrocarbons as diesel components.
  • a separator in which the mixture is sprayed by Venturi nozzles to to create a large evaporation surface.
  • the object of the present invention is to provide a method and a device which during operation to different
  • Residual compositions and residue throughputs is customizable
  • Hydrocarbon-containing composition has a boiling range of 170 ° C to 390 ° C and the hydrocarbons have 8 to 24 carbon atoms, and
  • the hydrocarbon-containing composition has a boiling range of 180 ° C to 320 ° C.
  • the Hydrocarbon compositions have a boiling range of 200 ° C to 280 ° C.
  • the hydrocarbons in the hydrocarbon-containing composition have 9 to 22, more preferably 10 to 20, carbon atoms.
  • the hydrocarbon-containing composition has a boiling range of 170 ° C to 390 ° C, preferably from 180 ° C to 320 ° C, more preferably 200 ° C to 280 ° C, wherein the hydrocarbons in the hydrocarbons -containing
  • the abovementioned hydrocarbons are preferably alkanes, cycloalkanes and / or aromatic hydrocarbons. According to a preferred embodiment, the aforementioned
  • Hydrocarbons preferably alkanes, cycloalkanes and aromatic hydrocarbons.
  • Composition to a diesel oil-containing composition preferably to diesel oil.
  • Diesel oil is also called diesel fuel.
  • Composition in a range of 35 to 100 wt .-%, more preferably from 40 to 90 wt .-%, even more preferably from 50 to 75 wt .-%, each based on the total weight of the hydrocarbon-containing
  • composition According to a further embodiment of the invention, the
  • Hydrocarbon-containing composition additionally 10 to 45, more preferably 15 to 40 wt .-%, even more preferably 25 to 38 wt .-%, still more preferably 30 to 35 wt .-%, fatty acid alkyl esters, each based on the total weight of the hydrocarbons containing composition.
  • the fatty acid alkyl esters preferably have an alkyl radical having 1 to 5 C atoms, preferably 1 to 4 C atoms, and a fatty acid radical having 10 to 30 C atoms, preferably 12 to 20 C atoms.
  • the fatty acid alkyl ester is
  • Fatty acid methyl ester Fatty acid methyl ester, fatty acid ethyl ester, fatty acid propyl ester and / or fatty acid butyl ester.
  • compositions are generally the above
  • Hydrocarbons-containing composition meant.
  • the waste oil to be treated is preferably
  • Lubricating oil and / or cooling oil in particular in the cooling and / or processing of metals, in particular of aluminum, preferably Aluminum ingot, obtained.
  • the lubricating and / or cooling oil can be mixed with water.
  • a water-containing oil has a water content in a range from 20 to 80 wt .-%, more preferably from 40 to 60 wt .-%, on.
  • the fluid is moved in a circuit.
  • the fluid flows not only once in the reactor device and in the
  • Composition is increased.
  • the fluid may further contain hydrocarbonaceous residues and / or
  • catalyst particles instead of admixed catalyst particles, for example, a stationary catalyst body may be provided. In an advantageous embodiment can be provided
  • Hydrocarbon-containing composition is possible.
  • the fluid can be fed tangentially to the fluidized-bed evaporator. It can be provided that the at least two initiation levels are arranged one above the other. The description of the location "on top of each other" is based on an evaporator with horizontally arranged discharge levels Furthermore, at least two inlets can be provided in each of the at least two discharge levels.
  • the at least two inlets are arranged at approximately constant angular distance from each other.
  • two inlets at an angular distance of 180 ° or three inlets with an angular spacing of 120 ° or four inlets with an angular spacing of 90 °, etc. may be provided. It is immaterial, with which tolerance the angular distances are formed.
  • a positive-conveying feed pump is used. Forced-conveying pumps are, for example, rotary piston pumps, progressing cavity pumps and gear pumps.
  • a controllable feed pump is used.
  • the fluid may have a viscosity in the range of 0.6 to 20 mPa »s, preferably from 1 to 12 MPa» s, still more preferably from 2 to 7 MPa 's have.
  • the volume flow through the reactor tubes can be adjusted in the range from 0.1 to 1000 m 3 / h, preferably from 100 to 600 m 3 / h, more preferably from 300 to 500 m 3 / h.
  • the pressure drop across the reactor tubes may be in the range of 0.5 to 40 bar, preferably 2 to 24 bar, more preferably 4 to 16 bar. The pressure drop across the reactor tubes determines the
  • the process may be by changing the capacity of the feed pump as a result of changing the feed pump and / or changing the operation of the feed pump and / or by changing the pressure drop across the
  • Reactor device by means of switching between parallel operation
  • Series operation of at least two reactor tubes are regulated.
  • hydrocarbon-containing residues are supplied to the fluid via a feed pipe ending in the evaporator.
  • Catalyst particles can be deposited in a solids separator.
  • the solids separator can be arranged in a bypass between the outlet of the feed pump and the inlet of the reactor device.
  • the catalyst used is preferably zeolite-based catalysts.
  • Suitable zeolites are preferably present in a proportion of 0.005 wt.% To 5.0 wt.%, More preferably in a proportion of 0.009 wt.% To 4.3 wt.%, More preferably in a proportion of 0, 01 wt .-% to 3.6 wt .-%, more preferably in a proportion of 0.03 wt .-% to 4.3 wt .-%, more preferably in a proportion of 0.05 wt .-% bis 1, 9 wt .-%, each based on the total weight of the fluid used. More preferably, the at least one zeolite is a zeolite Y, a zeolite X or a mixture thereof.
  • the at least one zeolite is a zeolite Y.
  • Zeolite Y is an artificially produced crystalline substance.
  • the crystal structure of the zeolite Y corresponds to that of Faujasith, wherein the Faujasithgerüst of sodalite cages, which are connected to each other via hexagonal prisms formed.
  • the at least one zeolite Y used comprises sodium or ammonium ions as counterions. In another preferred
  • the at least one zeolite used is a zeolite selected from the group consisting of NaY zeolite, 13X zeolite, 4A zeolite, 5A zeolite, NaX zeolite or mixtures thereof.
  • the at least one zeolite used is a NaY zeolite or a 13X zeolite or a zeolite
  • the zeolite used has an average size of less than 100 ⁇ m, more preferably less than 50 ⁇ m, more preferably less than 1 ⁇ m. More preferably, the zeolite used in the invention has a mean size of one
  • the process according to the invention can also be referred to as cracking process and the device as cracking device.
  • Hydrocarbons-containing composition has a boiling range of 170 ° C to 390 ° C and the hydrocarbons have 8 to 24 carbon atoms proposed, it being provided
  • the treatment plant a feed pump, a reactor device with comprising at least one reactor tube, a central container with an evaporator and a solids separator,
  • the central container is substantially formed as a hollow cylinder, and the evaporator forms the lower end portion of the central container, that the evaporator, preferably tangential, has inlets, which are arranged in at least two radial discharge planes,
  • the at least one inlets of adjacent discharge planes are arranged in such a way that they feed in different circumferential directions.
  • the evaporator as a
  • Fluidized bed evaporator is formed.
  • the fluid that has flowed into the evaporator has a very large evaporation surface, so that a high yield of a hydrocarbon-containing
  • Composition is possible.
  • the feed pump, the reactor device and the evaporator can be arranged in a fluid circuit one behind the other.
  • At least two inlets can be arranged in each of the at least two radial introduction levels. It can be provided that the at least two inlets are arranged at an approximately constant angular distance from each other. It can, for example, two inlets at an angular distance of 180 ° or three inlets with an angular distance of 120 ° or four inlets with a
  • Angular distance of 90 °, etc. may be provided. It is immaterial, with which tolerance the angular distances are formed.
  • At least two upper inlets are arranged in an upper introduction level and at least two lower inlets in a lower initiation level, and
  • extending supply pipes may be connected to a manifold which is connected to the outlet of the reactor unit.
  • the end portions of the inlets may be formed as a rectangular nozzle, preferably with an aspect ratio in the range of 3: 1 to 7: 1.
  • the end portions of the enemas are formed as helical swirl nozzles.
  • the swirl formed in the swirl nozzles intensifies the swirling of the fluid in the evaporator.
  • On the inner wall of the evaporator molding elements may be arranged.
  • the mold elements may have a curved cross section, for example, be formed as a half cylinder. It can also be provided that the Formelennente are formed as straight and / or curved baffles.
  • the form elements are extended over the entire height of the inner wall of the evaporator.
  • an entry basket may be arranged, in which a
  • Feed pipe opens, which is connected to the output of a Reststoffvorratsbehalters. From the residue reservoir can
  • hydrocarbon-containing residues are added to the fluid
  • the reactor device at least two
  • reactor tubes which are switchable from a parallel operation in a series operation and vice versa. By this switching, the effective length of the reactor tubes can be adapted to the operating requirements. It can be provided that the feed pump as a controllable
  • Feed pump is formed.
  • the feed pump has a drive motor whose speed is adjustable.
  • the feed pump can be designed as a forced-conveying pump, for example as a rotary piston pump, eccentric screw pump or gear pump. It can be provided that the solids separator in a switchable by means of valve means bypass between the output of the
  • the solids separator may be formed as a hydrocyclone.
  • FIG. 2a shows a first embodiment of a reactor tube device
  • FIG. 2b shows the reactor tube device in FIG. 2a with reactor tubes in FIG.
  • FIG. 3a shows a second embodiment of a reactor tube device with reactor tubes in parallel in a schematic
  • FIG. 3b shows the reactor tube device in FIG. 3a with reactor tubes in FIG.
  • FIG. 4 shows a first embodiment of an evaporator in a schematic front view
  • FIG. 5 shows the evaporator in FIG. 4 in a schematic plan view
  • FIG. 6 shows the evaporator in FIG. 4 in a schematic side view
  • FIG. Fig. 7 shows a second embodiment of an evaporator in one
  • FIG. 8 shows a third embodiment of an evaporator in a schematic plan view.
  • Fig. 1 shows a processing plant 1 for obtaining a
  • Hydrocarbon-containing composition has a boiling range of 170 ° C to 390 ° C and the hydrocarbons have 8 to 24 carbon atoms, from a circulating fluid comprising waste oil, organic residues and catalyst particles.
  • the waste oil is obtained, for example, in the cooling of aluminum ingots with an oil-water mixture in a rolling mill. During the cooling process, the chemical changes
  • composition of the oil used For reprocessing of the used oil-water mixture, for example, 60 to 80% vol. Has water, the waste oil is first separated from the water.
  • separated water can be purified in an oil-water separator or centrifuge in a separate process.
  • the processed in the processing plant 1 fluid can have a viscosity in the range of 0.6 to 20 mPa »s, preferably from 1 to 12 MPa» s, still more preferably from 2 to 7 MPa 's have.
  • the treatment plant 1 comprises a feed pump 2, a
  • Reactor device 3 with reactor tubes 31, a central container 4 with an evaporator 41 and a solids separator 5, wherein the fluid
  • Feed pump 2, the reactor device 3 and the evaporator 41 flows in a circuit.
  • the evaporator 41 is formed as a fluidized-bed evaporator 41 and will be referred to hereafter.
  • the reactor tubes 31 of the reactor device 3 the above-mentioned
  • the fluid is supplied through the arranged upstream of the reactor device 3 feed pump 2 mechanical energy, which provides the necessary heating and
  • Reactor tubes 31 is a pressure difference.
  • the catalytic reaction in which the long-chain organic constituents of the fluid are broken up into shorter-chain molecules with the assistance of the catalyst particles, that is to say cracked, takes place under the influence of the heat of friction developed by the mixing.
  • the fluid has at the outlet of the reactor tubes 31 a temperature in the range of 200 to 350 ° C, preferably from 240 to 310 ° C.
  • the heated fluid now enters tangentially into the fluidized-bed evaporator 41 arranged downstream of the reactor device 3.
  • Fluidized bed evaporator 41 forms the lower end portion of the im
  • End portion is formed as a conical steam cap 44, which merges into a hollow cylindrical distillation column 45.
  • Hydrocarbons containing composition is in a downstream of the capacitors 46 arranged product tank 6 collected. Exhaust gas over the hydrocarbonaceous composition is removed by means of a vacuum pump 7.
  • the central container 4 has an L-shaped feed pipe 47 for the provided in a residue reservoir 8 organic residues, which are supplied to the fluid circuit.
  • the feed tube 47 passes through the cylindrical portion of the central container 4 and opens in the
  • Fluidized bed evaporator 41 in a collection basket 48 (see Fig. 5).
  • the supplied via the feed tube 47 organic residues are doing in countercurrent process by ascending in the central container 4
  • the decrease passage-ready residual material through the grid meshes is thus significantly easier. It is also possible to dispense with the entry basket 48 and to input the residue material directly into the highly turbulent fluid region of the fluidized-bed evaporator 41.
  • the supplied organic residues are in the
  • Fluidized bed evaporator 41 is mixed with the remaining components of the fluid, which is now collected in a funnel-shaped bottom 4b of the central container 4 and is supplied via a pipe to the inlet of the downstream pump 2. This closes the fluid circuit.
  • Unreactable solids of the fluid and spent catalyst particles are removed from the fluid circuit in a solids separator 5, which may be a hydrocyclone.
  • the solids separator 5 is in a bypass between the output of the feed pump 2 and the input of the reactor device 3 is arranged.
  • the bypass is formed switchable via valve means 32.
  • the feed pump 2 is designed as a forced-conveying pump, for example as a rotary piston pump, eccentric screw pump or gear pump. Also suitable are centrifugal pumps, which are adapted to the reaction conditions according to their design; for example, free-flow pumps can be provided at elevated gas fractions of the fluid.
  • the downstream of the feed pump 2 arranged reactor device 3 is modular.
  • Each of the modules comprises in the embodiment of the treatment plant 1 shown in Fig. 1, two reactor tubes 31, valve means 32 and a connecting line 33. Per module, 2 to 9 reactor tubes 31 may be provided.
  • the reactor tubes 31 can be switched by means of the valve means 32 from a parallel operation to a series operation and vice versa. Several modules can be connected in parallel.
  • valve devices 32 can be used as individual valves, for example as
  • Wedge gate valves or segment valves, or as multiway valves are Wedge gate valves or segment valves, or as multiway valves,
  • the reactor tubes 31 are made of tubes having a diameter of 50 to 400 mm, preferably 150 to 250 mm, more preferably 200 mm.
  • the reactor tubes 31 have a length of 0.5 to 6 m, preferably from 2 to 4 m.
  • reactor tubes 31 are built-in elements, such as baffles,
  • Resistance elements, dividing and / or cutting elements are arranged, which homogenize and mix the fluid.
  • the mounting elements are not shown in Figs. 1 to 3.
  • Reactor tube 31 enters a characteristic pressure drop.
  • Operating points with respect to the pressure drop are in a range of 0.5 to 40 bar, preferably from 2 to 24 bar, more preferably from 4 to 16 bar.
  • the reactor tubes 31 have a characteristic plant characteristic
  • Reactor tubes 31 was a volume flow of 0.1 to 1000 m 3 / h
  • the reactor device 3 converts the generated by the feed pump 2 Flow energy into thermal energy, wherein the required
  • Reactor device 3 an ideal system for controlling the entry of the reaction energy.
  • the energy introduced into the fluid can be determined via the pump input power, where:
  • Feed rate volume flow * pressure loss
  • the volume flow is adjustable via the feed pump 2, the pressure loss is adjustable by the reactor tubes 31.
  • the pressure loss by varying the effective length of the reactor tubes 31 by means of the above-described switching from parallel operation in series operation and vice versa adjustable.
  • the treatment plant 1 is quickly adaptable to changing operating conditions, such as viscosity changes of the fluid and changes in the composition of the reaction mass.
  • Figs. 2a and 2b show a first embodiment of the
  • Reactor device 3 with a module having two reactor tubes 31 and wherein the valve means 32 are formed as individual valves.
  • the reactor device 3 has longitudinal valves 32I, which are respectively arranged at the inlet and the outlet of the reactor tubes 31, and transverse valves 32q, each at the inlet and at the outlet of the connecting pipe 33 are arranged. For a better understanding blocked valves are highlighted in black.
  • the two reactor tubes 31 are connected in parallel operation: the longitudinal valves 32I are opened, and the transverse valves 32q are blocked.
  • the two reactor tubes are connected in series operation: arranged at the output of the right reactor tube longitudinal valve 32I is disabled, arranged at the input and output of the connecting line 33 cross valve 32q are open and that at the entrance of the left reactor tube 31st arranged longitudinal valve 311 is locked. Consequently, the fluid conveyed by the feed pump 2 flows through the right reactor tube 31, the connection pipe 33, the left one, via the longitudinal valve 311 located at the entrance of the right reactor tube 31 and opened
  • Reactor tube 31 and arranged at the outlet of the left reactor tube 31 and opened longitudinal valve 311 in the fluidized bed evaporator 41st
  • FIGS. 3a and 3b show a second embodiment of the invention
  • Reactor device 3 which is designed as the embodiment described in Fig. 2, with the difference that the valve means 32 are formed as three-way valves 32d.
  • the three-way valves 32 d are respectively arranged at the inlet and the outlet of the reactor tubes 31.
  • the three-way valve 32d disposed at the exit of the right reactor tube 31 is further connected to the entrance of the communication passage 33, and the three-way valve 32d located at the entrance of the left reactor tube 31 is further connected to the exit of the communication passage 33.
  • the two reactor tubes 31 are connected in parallel operation: the three-way valves 32d are switched to passage that the flow through the connecting line 33 is interrupted.
  • the two reactor tubes are connected in series operation: the arranged at the outlet of the right reactor tube 31 three-way valve 32 d is connected so that it blocks the introduction of fluid flow into the fluidized bed evaporator 41 and the path through the connecting line 33 releases and the three-way valve 32 d arranged at the entrance of the left reactor tube 31 is connected to block the inflow from the feed pump 2 and to connect the output of the connection line 33 to the inlet of the left reactor tube 31.
  • the fluid delivered by the delivery pump 2 flows through the three-way valve 31d provided at the entrance of the right reactor tube 31 through the right reactor tube 31, the connection line 33, the left reactor tube 31, and the three-way valve 31d located at the exit of the left reactor tube 31
  • FIGS. 4 to 6 show the construction of the fluidized-bed evaporator 41, which, as described above, forms the lower end section of the substantially hollow-cylindrical central container 4.
  • the fluid is fed to the fluidized-bed evaporator 41 via tangential inlets 41 1, which are arranged in radial discharge planes 412.
  • tangential inlets 41 1 In a radial introduction level 412 two inlets 41 1 are arranged opposite each other. At least two preamble planes 412 are provided which are spaced from each other.
  • two superimposed initiation levels 412 are provided in the in Fig. 4 to 6 illustrated embodiment of the fluidized-bed evaporator 41.
  • An upper initiation plane 412o is in the upper end portion of the
  • Fluidized bed evaporator 41 is arranged, and a lower introduction level 412u is disposed in the lower end portion of the fluidized-bed evaporator 41.
  • the inlet 41 1 o, 41 1 u of the initiation levels 412o, 412u are oriented so that they feed in the same direction of rotation, the direction of rotation in the two initiation levels 412o, 412u are opposite to each other.
  • the supplied fluid is set in rotation and forms vortices which rotate about the center axis of the fluidized-bed evaporator 41.
  • the injected fluid is so intensively swirled by the turbulent flow formed in the fluid that a large evaporation surface is formed.
  • the volume flow V [m 3 / h] of the circulating fluid conducted through the fluidized-bed evaporator 41 is related to the inner diameter D [m] in the following manner:
  • the number of tangential inlets 41 1 and / or the introduction levels 412 can be controlled via valve devices.
  • the end portions of the inlet 41 1 can have different shapes
  • each of the inlets 41 1 It has been proven to dimension each of the inlets 41 1 so that when opening all enemas 41 1 a minimum flow rate of the fluid in the range of 1 to 20 m / s, preferably from 2 to 10 m / s, more preferably from 3 to 5 m / s is present. When individual inlets 41 1 are closed, the flow rates of the remaining open inlets 41 1 increase.
  • an upper inlet 41 1 o and a lower inlet 41 1 u are connected to one another on each side of the fluidized-bed evaporator 41 by an obliquely extending lateral feed pipe 42.
  • the lateral supply pipes 42 are centered with the output side
  • FIGS. 4 to 6 show embodiments of the fluidized-bed evaporator 41, in which the inner wall of the fluidized-bed evaporator 41 is not smooth as in the embodiment described above in FIGS. 4 to 6, but structured, by forming elements 41 f on the inner wall of the fluidized-bed evaporator 41 .
  • the shaping elements 41 f cause wall-near fluid flows to swirl even more intensively.
  • the shaped elements 41 f may, for example, have a curved cross-section (see FIG. 7) or be formed as straight and / or curved baffles (see FIG Fig. 8).
  • the Fornnelennente 41 f may be formed over the entire surface or have breakouts.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé et un dispositif d'obtention d'une composition contenant des hydrocarbures à partir d'un fluide comprenant de l'huile usagée, la composition contenant des hydrocarbures ayant un point d'ébullition dans la plage de 170 à 390°C et les hydrocarbures portant de 8 à 24 atomes de carbone. Au moyen d'une pompe d'alimentation (2), on injecte de l'énergie dans le fluide. On mélange le fluide dans un système de réacteur (3) constitué d'au moins un tube réactionnel (31) et on le chauffe au moyen de l'énergie injectée, puis on traite d'huile usagée pour donner la composition contenant des hydrocarbures. On amène le fluide chauffé dans des plans d'introduction (412) radiaux à un évaporateur (41) qui dispose d'au moins deux plans d'introduction (412), le sens de rotation étant différent dans des plans d'introduction adjacents, et on évapore la composition contenant des hydrocarbures. Chacun des plans d'introduction (412) comporte au moins une admission (411).
PCT/EP2013/065329 2013-07-19 2013-07-19 Procédé et dispositif d'obtention d'une composition contenant des hydrocarbures à partir de résidus Ceased WO2015007343A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/EP2013/065329 WO2015007343A1 (fr) 2013-07-19 2013-07-19 Procédé et dispositif d'obtention d'une composition contenant des hydrocarbures à partir de résidus

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Application Number Priority Date Filing Date Title
PCT/EP2013/065329 WO2015007343A1 (fr) 2013-07-19 2013-07-19 Procédé et dispositif d'obtention d'une composition contenant des hydrocarbures à partir de résidus

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US11591528B2 (en) 2017-12-13 2023-02-28 Karl Ip Holdings Inc. Low-pressure catalytic conversion of used motor oil to diesel fuel

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US11591528B2 (en) 2017-12-13 2023-02-28 Karl Ip Holdings Inc. Low-pressure catalytic conversion of used motor oil to diesel fuel

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